US4333824A - Refining highly aromatic lube oil stocks - Google Patents

Refining highly aromatic lube oil stocks Download PDF

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Publication number
US4333824A
US4333824A US06/163,571 US16357180A US4333824A US 4333824 A US4333824 A US 4333824A US 16357180 A US16357180 A US 16357180A US 4333824 A US4333824 A US 4333824A
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US
United States
Prior art keywords
solvent
extract
pyrrolidone
methyl
extraction zone
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Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
Application number
US06/163,571
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English (en)
Inventor
William F. Brown
Albert G. Bieber
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Bechtel Corp
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Texaco Inc
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Texaco Inc filed Critical Texaco Inc
Priority to US06/163,571 priority Critical patent/US4333824A/en
Priority to JP6355681A priority patent/JPS5714688A/ja
Priority to GB8118681A priority patent/GB2078778B/en
Priority to FR8112091A priority patent/FR2485562A1/fr
Priority to CA000380482A priority patent/CA1164391A/en
Priority to AU72107/81A priority patent/AU540199B2/en
Priority to DE19813124783 priority patent/DE3124783A1/de
Priority to BE0/205214A priority patent/BE889385A/fr
Priority to IT22551/81A priority patent/IT1137257B/it
Priority to BR8104046A priority patent/BR8104046A/pt
Priority to YU1601/81A priority patent/YU41524B/xx
Priority to MX819511U priority patent/MX7275E/es
Priority to ES503457A priority patent/ES8300839A1/es
Priority to NL8103107A priority patent/NL8103107A/nl
Application granted granted Critical
Publication of US4333824A publication Critical patent/US4333824A/en
Assigned to BECHTEL CORPORATION reassignment BECHTEL CORPORATION ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: TEXACO INC.
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
    • C10G21/28—Recovery of used solvent

Definitions

  • This invention relates to an improved process for the solvent extraction of a highly aromatic petroleum oil fraction containing aromatic and non-aromatic components.
  • the invention relates to a method for solvent extraction of lubricating oil stocks with a highly selective solvent, i.e., N-methyl-2-pyrrolidone, at a low solvent to oil dosage, employing a portion of the extract oil product as a solvent modifier with a resultant savings in energy as compared with solvent refining processes employing N-methyl-2-pyrrolidone with water as the solvent modifier.
  • a highly selective solvent i.e., N-methyl-2-pyrrolidone
  • aromatic and unsaturated components of a lubricating oil base stock such as those derived from crude petroleum by fractional distillation, may be separated from the more saturated hydrocarbon components by various processes involving solvent extraction of the aromatic and unsaturated hydrocarbons.
  • solvent extraction of the aromatic and unsaturated hydrocarbons.
  • the removal of aromatics and other undesirable constituents from lubricating oil base stocks improves the viscosity index, color, oxidative stability, thermal stability, and inhibition response of the base oils and the ultimate lubricating oil products.
  • a process which has received widespread commercial acceptance employs N-methyl-2-pyrrolidone as solvent.
  • the process of the present invention employs N-methyl-2-pyrrolidone modified by the addition of 0.5 to 3 weight percent extract oil as a solvent modifier for solvent extraction of highly aromatic feedstocks, such as those derived from Arabian Light crude oils.
  • N-methyl-2-pyrrolidone is chemically stable, has low toxicity, and has the ability to produce refined oils of improved quality as compared with other known solvents.
  • the solvent extraction step is carried out under conditions effective to recover about 30 to 90 volume percent of the lubricating oil charge as raffinate or refined oil and to extract about 10 to 70 volume percent of the charge as an aromatic extract.
  • the lubricating oil stock is contacted with the solvent, N-methyl-2-pyrrolidone, at a temperature at least 10° C., preferably at least 50° C., below the temperature of complete miscibility of the lubricating oil stock in the solvent.
  • solvent extraction temperatures are generally within the range of 43° to 100° C. (110° to 212° F.), preferably within the range of 54° to 95° C. (130° to 205° F.), with solvent dosages within the range of 50 to 500 volume percent, and preferably within the range of 100 to 300 volume percent.
  • the primary raffinate is dewaxed to the desired pour point.
  • the refined or dewaxed oil may be subjected to a finishing treatment for color and stability improvement, for example, mild hydrogenation.
  • the present invention provides an improvement in the solvent refining of lubricating oil stocks with N-methyl-2-pyrrolidone extraction processes wherein the solvent power of the N-methyl-2-pyrrolidone is modified without the need for water as a moderator. This is accomplished by returning part of the extract, to the extraction step.
  • the recycle extract is separated from the primary extract mix and returned to the extraction zone admixture with substantially dry N-methyl-2-pyrrolidone solvent.
  • extract may be recycled to the extraction zone to displace non-aromatic hydrocarbons from the extract phase in known manner.
  • the solvent recycled to the extraction zone may be further modified by adding a portion of the raffinate to the mixture of recycled solvent and extract.
  • FIG. 1 of the drawings is a schematic flow diagram illustrating a solvent refining process embodying the improved process of this invention.
  • FIG. 2 is a graphic illustration of the relationship between solvent dosage and refined oil quality as represented by its refractive index for dry N-methyl-2-pyrrolidone (MP) and for N-methyl-2-pyrrolidone modified by the addition of extract.
  • FIG. 3 is a similar graphic illustration showing the relationship between viscosity index of the refined oil and refined oil yield for the solvent systems of FIG. 2.
  • FIG. 1 of the drawing a preferred embodiment of the subject invention is disclosed as applied to solvent refining highly aromatic lubricating oil feedstocks.
  • Lubricating oil feedstock enters the system through line 5 and is introduced into extraction tower 6 where it is brought into intimate countercurrent contact with N-methyl-2-pyrrolidone introduced into the upper portion of the extraction tower through line 7.
  • Extraction tower 6 typically operates at a pressure in the range of 550 to 1000 kPa (80 to 145 psia).
  • An extract mixture typically comprising about 85 percent solvent is withdrawn from the bottom of extraction tower 6 through line 8.
  • a raffinate mixture, comprising typically 85 percent hydrocarbon oil admixed with solvent is discharged from the extraction tower 6 through line 8 and processed for the recovery of raffinate from the solvent as described hereinafter.
  • the major portion of the solvent appears in the extract mixture withdrawn from the bottom of extraction tower 6 through line 8.
  • the extract mixture is processed first for the recovery of solvent from the extract and then for recovery of the extract as a marketable product of the process.
  • the extract mixture typically containing about 85 percent of the solvent, is passed through line 8 and heat exchangers 10 and 11 which serve to preheat the extract mixture, and introduced into the upper part of a low pressure flash tower 12.
  • Flash tower 12 typically operates at a pressure 108 to 136 kPa (1 to 5 psig).
  • Solvent is introduced into the upper part of tower 12 as reflux through line 13.
  • Solvent separated from the extract in flash tower 12 is discharged through line 14 to heat exchanger 10 wherein it is cooled by indirect heat exchange with the extract mixture from extraction tower 6 thereby preheating the extract mixture prior to introduction to flash tower 12 and condensing solvent vapors.
  • the solvent is further cooled and condensed in a cooler 16 and passed through line 17 to solvent purification and storage system 68 described in more detail hereinafter.
  • the unvaporized portion of the extract mixture is withdrawn from the bottom of flash tower 12 by pump 19 and passed through a heater 21 wherein it is heated to an elevated temperature, and introduced through line 22 to a high pressure flash tower 24.
  • the high pressure flash tower 24 suitably is maintained at a pressure within the range of 375 to 415 kPa (40 to 45 psig) and is provided with a reflux of solvent which enters the upper part of tower 24 through line 26.
  • a further amount of solvent is separated from the extract in tower 24, the solvent rich vapors leaving the top of the tower through line 27.
  • Part of the vapors from line 27 are passed through line 28 to heat exchanger 11 for indirect heat exchange with extract mixture from the lower part of extraction tower 6, serving to condense the solvent vapors and preheat the extract mixture prior to its introduction to column 12.
  • the condensed solvent is passed through line 28 to solvent purification and storage as described hereinafter.
  • the remainder to the solvent vapors passing overhead from high pressure separator 24 pass through line 29 to the solvent purification and storage system.
  • the hydrocarbon oil extract is withdrawn from the lower portion of high pressure flash tower 24.
  • a portion of the extract mixture from flash tower 24 may be passed through cooler 30 and line 30' to the lower part of extraction tower 6.
  • a portion of the extract mixture from flash tower 24 may be passed through cooler 30 and line 30" to line 71 and introduced into extraction tower 6 in admixture with recycle solvent.
  • the remainder passes through line 31 to vacuum flash tower 32.
  • Vacuum flash tower 32 typically is a countercurrent vapor-liquid contact device suitably provided with a cascade or bubble trays. Dry solvent is introduced near the top of the tower 32 through line 33 as reflux.
  • Stripper 41 is typically a countercurrent vapor-liquid contact column provided with bubble trays in which the liquid extract flowing downwardly through the tower is contacted with inert stripping gas or steam introduced into the lower portion of the stripper 41 through line 42.
  • Solvent is introduced near the top of stripping column 41 through line 43 as reflux. Extract oil containing less than about 50 parts per million solvent and typically comprising 80 percent unsaturated hydrocarbons and about 20 percent saturated hydrocarbons is withdrawn from the lower part of stripper 41 by pump 44 and discharged through line 45 as a product of the process.
  • Solvent vapors mixed with stripping medium i.e., inert gas or steam, and usually containing also some light oil carried over from the flash tower and stipper, are discharged from the upper part of the stripper 41 through line 46 to condenser 47 and solvent accumulator 48. Condensate is separated from uncondensible gases in solvent accumulator 48, and the gases are withdrawn from accumulator 48 through line 49 to a vacuum system not illustrated in the drawing.
  • the raffinate mixture leaving the top of the extraction column 6 through line 9 is passed through a heat exchanger 51 and heater 52 wherein the raffinate mixture is heated, and then introduced into a vacuum flash tower 53, similar to vacuum flash tower 32, previously described.
  • Vacuum flash tower 53 is provided with a means for the introduction of solvent through line 54 to the upper portion of the tower as reflux. Solvent vapors are taken overhead from flash tower 53 to line 34 for recovery together with solvent from flash tower 32.
  • the unvaporized portion of the raffinate mixture is withdrawn from the bottom of vacuum flash tower 54 through line 56 and introduced into the upper portion of a stripping column 57 similar to stripping column 41, previously described.
  • Solvent is introduced into stripper 57 as a reflux through line 58 and a stripping medium, e.g., inert gas or steam, is introduced near the bottom of the stripper through line 59. Stripping medium and solvent vapors are discharged from stripper 57 through lines 61 and 46 to condenser 47 for recovery together with the stripping medium and solvent from stripper 41.
  • a stripping medium e.g., inert gas or steam
  • a portion of the raffinate mixture from the bottom of vacuum flash tower 54 may be passed through line 60 and cooler 60' to line 71 and introduced into extraction tower 6 in admixture with recycle solvent.
  • the bottoms product from stripper 57 is passed by a pump 62 through line 63 to heat exchanger 51 where it is cooled by indirect heat exchange with the incoming feed to the vacuum flash tower 53 and is discharged through line 65 as solvent refined lubricating oil base stock, the principal product of the process.
  • product raffinate may be passed through line 65' to cooler 61' for recycle to extraction tower 6 with recycle solvent from line 71.
  • Condensate from accumulator drums 37 and 48 are passed by pumps 66 and 67, respectively, to a solvent purification and storage system 68.
  • Various process steps may be utilized in the purification of solvent for reuse in the process, including, for example, distillation, gas stripping, and the like, primarily for removal of water, if present, and for removal of polymers, oils, and other undesirable constituents.
  • Condensate water from stripping or excess water from an extraneous source may be removed from the solvent in the solvent purification system 68 and discharged through line 69. Solvent is recycled to the process by pump 70 through line 71 to lines 7, 13, 26, 33, 43, 54 and 58 as required.
  • partially stripped extract from high pressure flash tower 24 is recirculated to extraction tower 6 via line 30" in an amount sufficient to provide from 0.5 to 3 weight percent, preferably from 1 to 2 weight percent extract reckoned on a solvent-free basis in the recycled solvent to the extraction tower.
  • test runs were carried out to determine the effect of adding extract oil to N-methyl-2-pyrrolidone as solvent in the refining of lubricating oil base stocks.
  • the test runs were carried out in a twelve-stage countercurrent contactor with the feed entering stage six and the solvent entering stage twelve.
  • Extract is withdrawn at stage one and raffinate, at stage twelve.
  • the raffinate product was then dewaxed and tested for viscosity index and ASTM pour point.
  • Runs 1 to 16 inclusive runs were conducted with a Wax Distillate-5 (WD-5) as the hydrocarbon feed.
  • WD-5 Wax Distillate-5
  • Runs 5 to 16 various amounts of the extract from the respective runs, ranging from 0.5 weight percent to 2 weight percent, were added to the N-methyl-2-pyrrolidone solvent supplied to the extraction zone. Operating conditions and results are shown in Table I.
  • the solvent composition comprises 1 to 2 weight percent extract from the feedstock undergoing solvent refining, with some reduction in product quality as indicated by the refractive index at 70° C. (RI 70 ) of the raffinate and the viscosity index of the dewaxed oil.
  • RI 70 refractive index at 70° C.
  • a Wax Distillate-20 (WD-20) lubricating oil base stock was treated with substantially pure (99.7 percent) N-methyl-2-pyrrolidone substantially free from water (0.1 weight percent water), and with mixtures of N-methyl-2-pyrrolidone and WD-20 extract from the respective runs.
  • the process of this invention provides a means for increasing the yield of refined oil product from highly aromatic feedstocks at relatively low to moderate solvent-to-oil dosages without the need for water as a solvent moderator.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Lubricants (AREA)
  • Pyrrole Compounds (AREA)
US06/163,571 1980-06-27 1980-06-27 Refining highly aromatic lube oil stocks Expired - Lifetime US4333824A (en)

Priority Applications (14)

Application Number Priority Date Filing Date Title
US06/163,571 US4333824A (en) 1980-06-27 1980-06-27 Refining highly aromatic lube oil stocks
JP6355681A JPS5714688A (en) 1980-06-27 1981-04-28 Solvent purification of oil stock material
GB8118681A GB2078778B (en) 1980-06-27 1981-06-17 Refining highly aromatic lube oil stocks
FR8112091A FR2485562A1 (fr) 1980-06-27 1981-06-19 Procede de raffinage de fractions d'huiles lubrifiantes a forte teneur en aromatiques
AU72107/81A AU540199B2 (en) 1980-06-27 1981-06-24 Solvent refining of a petroleum based oil stock with n-methyl 2-pyrrolidone
DE19813124783 DE3124783A1 (de) 1980-06-27 1981-06-24 "verfahren zur loesungsmittelextraktion von mineraloelfraktionen"
CA000380482A CA1164391A (en) 1980-06-27 1981-06-24 Refining highly aromatic lube oil stocks
IT22551/81A IT1137257B (it) 1980-06-27 1981-06-25 Raffinazione di cariche di oli lubrificanti ad alto tenore di aromatici
BE0/205214A BE889385A (fr) 1980-06-27 1981-06-25 Procede de raffinage par solvant d'huiles de petrole a forte teneur en aromatiques
BR8104046A BR8104046A (pt) 1980-06-27 1981-06-26 Processo para refinacao,com solvente,de uma carga de oleo a base de petroleo e processo para extracao,com solvente,de uma mistura de hidrocarbonetos
YU1601/81A YU41524B (en) 1980-06-27 1981-06-26 Process for solvent extracting of a high aromatic fraction of petroleum oil containing aromatic and nonaromatic components
MX819511U MX7275E (es) 1980-06-27 1981-06-26 Procedimiento mejorado para la extraccion con disolvente de una fraccion de hidrocarburos aromaticos de una mezcla de hidrocarburos aromaticos y no aromaticos
ES503457A ES8300839A1 (es) 1980-06-27 1981-06-26 Un procedimiento para el refino con disolvente de un mate- rial de aceite a base de petroleo
NL8103107A NL8103107A (nl) 1980-06-27 1981-06-26 Werkwijze voor het raffineren van sterk aromatische smeerolie voorraden.

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
US06/163,571 US4333824A (en) 1980-06-27 1980-06-27 Refining highly aromatic lube oil stocks

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US4333824A true US4333824A (en) 1982-06-08

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US06/163,571 Expired - Lifetime US4333824A (en) 1980-06-27 1980-06-27 Refining highly aromatic lube oil stocks

Country Status (14)

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US (1) US4333824A (es)
JP (1) JPS5714688A (es)
AU (1) AU540199B2 (es)
BE (1) BE889385A (es)
BR (1) BR8104046A (es)
CA (1) CA1164391A (es)
DE (1) DE3124783A1 (es)
ES (1) ES8300839A1 (es)
FR (1) FR2485562A1 (es)
GB (1) GB2078778B (es)
IT (1) IT1137257B (es)
MX (1) MX7275E (es)
NL (1) NL8103107A (es)
YU (1) YU41524B (es)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4909927A (en) * 1985-12-31 1990-03-20 Exxon Research And Engineering Company Extraction of hydrocarbon oils using a combination polar extraction solvent-aliphatic-aromatic or polar extraction solvent-polar substituted naphthenes extraction solvent mixture
US6123835A (en) * 1997-06-24 2000-09-26 Process Dynamics, Inc. Two phase hydroprocessing
US20050082202A1 (en) * 1997-06-24 2005-04-21 Process Dynamics, Inc. Two phase hydroprocessing
US9096804B2 (en) 2011-01-19 2015-08-04 P.D. Technology Development, Llc Process for hydroprocessing of non-petroleum feedstocks
US20180339243A1 (en) * 2015-11-10 2018-11-29 Hindustan Petroleum Corporation Limited A composition and a process for reducing aromatics from a hydrocarbon feedstock

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3207404A1 (de) * 1982-03-02 1983-09-08 Metallgesellschaft Ag, 6000 Frankfurt Verfahren zur entfernung von aromatischen verbindungen aus kohlenwasserstoffen
EP0098359A3 (en) * 1982-07-06 1984-03-07 Texaco Development Corporation Recovery for solvent from a hydrocarbon extract

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2771494A (en) * 1953-03-12 1956-11-20 Phillips Petroleum Co Selective solvent extraction of naphthene hydrocarbons employing 2-pyrrolidone
US3299158A (en) * 1960-06-04 1967-01-17 Metallgesellschaft Ag Production of pure aromatic hydrocarbons
US3451925A (en) * 1967-03-13 1969-06-24 Nixon Roberta L Solvent extraction of hydrocarbons with n-methyl-2-pyrrolidone
US3461066A (en) * 1966-12-23 1969-08-12 Texaco Inc Solvent recovery in the solvent extraction of hydrocarbon oils
US3721620A (en) * 1969-07-18 1973-03-20 Snam Progetti Process for the extraction of aromatic hydrocarbons
US3755154A (en) * 1969-12-10 1973-08-28 Nissan Chemical Ind Ltd Separation of hydrocarbons from mixture thereof

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3422163A (en) * 1965-10-21 1969-01-14 Universal Oil Prod Co Recovery of aromatics from multiple hydrocarbon streams
US3361664A (en) * 1966-04-05 1968-01-02 Universal Oil Prod Co Flashing and extractively distilling an extract
NL165940C (nl) * 1969-11-28 1981-06-15 Shell Int Research Werkwijze voor het scheiden van een mengsel van aromatische en niet-aromatische koolwaterstoffen met behulp van meertraps-vloeistof/vloeistofextractie, alsmede inrichting geschikt voor het uitvoeren van de werkwijze.

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2771494A (en) * 1953-03-12 1956-11-20 Phillips Petroleum Co Selective solvent extraction of naphthene hydrocarbons employing 2-pyrrolidone
US3299158A (en) * 1960-06-04 1967-01-17 Metallgesellschaft Ag Production of pure aromatic hydrocarbons
US3461066A (en) * 1966-12-23 1969-08-12 Texaco Inc Solvent recovery in the solvent extraction of hydrocarbon oils
US3451925A (en) * 1967-03-13 1969-06-24 Nixon Roberta L Solvent extraction of hydrocarbons with n-methyl-2-pyrrolidone
US3721620A (en) * 1969-07-18 1973-03-20 Snam Progetti Process for the extraction of aromatic hydrocarbons
US3755154A (en) * 1969-12-10 1973-08-28 Nissan Chemical Ind Ltd Separation of hydrocarbons from mixture thereof

Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4909927A (en) * 1985-12-31 1990-03-20 Exxon Research And Engineering Company Extraction of hydrocarbon oils using a combination polar extraction solvent-aliphatic-aromatic or polar extraction solvent-polar substituted naphthenes extraction solvent mixture
US6123835A (en) * 1997-06-24 2000-09-26 Process Dynamics, Inc. Two phase hydroprocessing
US6428686B1 (en) * 1997-06-24 2002-08-06 Process Dynamics, Inc. Two phase hydroprocessing
US6881326B2 (en) 1997-06-24 2005-04-19 Process Dynamics, Inc. Two phase hydroprocessing
US20050082202A1 (en) * 1997-06-24 2005-04-21 Process Dynamics, Inc. Two phase hydroprocessing
US7291257B2 (en) 1997-06-24 2007-11-06 Process Dynamics, Inc. Two phase hydroprocessing
US9096804B2 (en) 2011-01-19 2015-08-04 P.D. Technology Development, Llc Process for hydroprocessing of non-petroleum feedstocks
US9828552B1 (en) 2011-01-19 2017-11-28 Duke Technologies, Llc Process for hydroprocessing of non-petroleum feedstocks
US10961463B2 (en) 2011-01-19 2021-03-30 Duke Technologies, Llc Process for hydroprocessing of non-petroleum feedstocks
US20180339243A1 (en) * 2015-11-10 2018-11-29 Hindustan Petroleum Corporation Limited A composition and a process for reducing aromatics from a hydrocarbon feedstock
US10881984B2 (en) * 2015-11-10 2021-01-05 Hindustan Petroleum Corporation Limited Composition and a process for reducing aromatics from a hydrocarbon feedstock

Also Published As

Publication number Publication date
IT8122551A0 (it) 1981-06-25
FR2485562B1 (es) 1984-12-14
AU540199B2 (en) 1984-11-08
FR2485562A1 (fr) 1981-12-31
AU7210781A (en) 1982-01-07
JPS5714688A (en) 1982-01-25
ES503457A0 (es) 1982-11-01
NL8103107A (nl) 1982-01-18
BR8104046A (pt) 1982-03-16
CA1164391A (en) 1984-03-27
YU160181A (en) 1983-06-30
GB2078778A (en) 1982-01-13
YU41524B (en) 1987-08-31
MX7275E (es) 1988-03-28
IT1137257B (it) 1986-09-03
BE889385A (fr) 1981-12-28
GB2078778B (en) 1984-01-25
ES8300839A1 (es) 1982-11-01
DE3124783A1 (de) 1982-06-03

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